EP0530696A2 - Process for the preparation of pentane 1,5-diamines - Google Patents
Process for the preparation of pentane 1,5-diamines Download PDFInfo
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- EP0530696A2 EP0530696A2 EP92114711A EP92114711A EP0530696A2 EP 0530696 A2 EP0530696 A2 EP 0530696A2 EP 92114711 A EP92114711 A EP 92114711A EP 92114711 A EP92114711 A EP 92114711A EP 0530696 A2 EP0530696 A2 EP 0530696A2
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C209/00—Preparation of compounds containing amino groups bound to a carbon skeleton
- C07C209/44—Preparation of compounds containing amino groups bound to a carbon skeleton by reduction of carboxylic acids or esters thereof in presence of ammonia or amines, or by reduction of nitriles, carboxylic acid amides, imines or imino-ethers
- C07C209/48—Preparation of compounds containing amino groups bound to a carbon skeleton by reduction of carboxylic acids or esters thereof in presence of ammonia or amines, or by reduction of nitriles, carboxylic acid amides, imines or imino-ethers by reduction of nitriles
Definitions
- the present invention relates to a new process for the preparation of aliphatic pentane-1,5-diamines from gamma-cyanoketones and new pentane-1,5-diamines.
- 1,5-diaminohexane from Chem. Ber. 3387 to 3389 (1966) the production of 1,5-diaminohexane from 5-oxocapronitrile is known. Thereafter, 1,5-diaminohexane is obtained only via the intermediate stage of the oxime by first reacting 5-oxocapronitrile with hydroxylamine hydrochloride in the presence of anhydrous sodium carbonate to give 5-oximinocapronitrile and then reducing this to lithium diamine with lithium aluminum hydride; the overall yield is 42%. According to the authors, direct aminating hydrogenation of 5-oxo-capronitrile leads to the cyclization product, 2-methylpiperidine.
- EP-A-42 119 describes a process for the preparation of primary mono- and diamines from oxo compounds, which may also contain other groups capable of reduction, with ammonia and hydrogen in the presence of known hydrogenation catalysts, in which prior to the reaction with ammonia and hydrogen in the presence of hydrogenation catalysts, the oxo compounds at temperatures from 10 to 200 ° C and pressures from 1 to 300 bar a prereaction with ammonia in the presence of inorganic and organic ion exchangers in the ammonium form as imine formation catalysts.
- the present invention was therefore based on the object of finding a process for the preparation of pentane-1,5-diamines which alleviates the disadvantages mentioned above, in particular from producing ⁇ -cyanoketones under technically practicable conditions, with technically satisfactory yields or space-time yields and new pentane-1,5-diamines with - compared to the known 1,5-hexanediamine - higher degree of substitution.
- Process steps a and b can also be carried out in a reactor in which imination catalysts and hydrogenation catalysts are arranged in two separate layers.
- the imination is advantageously carried out in the presence of hydrogen.
- the starting materials for the process are e.g. accessible from ketones and acrylonitrile.
- the process according to the invention thus enables the conversion of the ⁇ -cyanoketones in high yields and space-time yields to the pentane-1,5-diamines.
- the substituents R1 'to R3' in the compounds I ' have the same meaning as the substituents R1 to R3 in the compounds I, with the proviso that R1' is not methyl when R2 'and R3' is hydrogen.
- Preferred ⁇ -cyanoketones of the general formula II are, for example: 5-oxohexanenitrile (from acetone), 4-methyl-5-oxo-hexanenitrile (from methyl ethyl ketone), 4-methyl-5-oxo-heptanenitrile (from diethyl ketone), 4-ethyl-5-oxo-hexanenitrile (from methyl propyl ketone), 4,4-dimethyl-5-oxo-hexanenitrile (from methyl isopropyl ketone), 4,4-dimethyl-5-oxo-heptanenitrile (from ethyl isopropyl ketone), 4,4,5-trimethyl-5-oxo-heptanenitrile (from diisopropyl ketone), 4-isoproypl-5-oxo-hexanenitrile (from methyl isobutyl ketone), 4-isopropenyl-5-oxo-
- the claimed diamines are distinguished from the known 1,5-hexanediamine by virtue of the higher degree of substitution by lower volatility and greater asymmetry (different reactivity of the amine functions). This results in easy processing of the diamines, for example as components (hardeners) for epoxies and components for polyamides and less odor nuisance due to unreacted diamines and the diisocyanates that can be produced from them.
- a vertical tubular reactor (diameter: 16 mm, filling height: 50 cm, oil-heated double jacket) was filled with 90.1 g (87 ml) of a catalyst with 3% ruthenium on ⁇ -aluminum oxide in the form of 1.2 mm strands (catalyst preparation by Pore impregnation of ⁇ -aluminum oxide with aqueous ruthenium nitrate solution and drying at 120 ° C).
- the catalyst was kept at 100 bar for reduction with simultaneous passage of 150 Nl / h of hydrogen after gradually increasing the temperature from 100 to 220 ° C. within 7 h 9 h at 220 ° C.
- a tube reactor (diameter: 16 mm, filling height: 50 cm, oil-heated double jacket), which was filled with 65.3 g (100 ml) of titanium dioxide (anatase) in the form of 1.5 mm strands, was passed through a tube reactor upstream of the hydrogenation reactor at a pressure of 250 bar and a temperature of 80 ° C, 20.5 g of 5-oxo-hexanenitrile (purity 97.7%) and 240 g of liquid ammonia are pumped every hour. The discharge was then passed through the hydrogenation reactor from bottom to top at a pressure of 250 bar and a temperature of 110 ° C. while simultaneously passing 100 Nl / h of hydrogen through it. After relaxing to normal pressure, NH3 was distilled off and the hydrogenation output was analyzed with quantitative gas chromatography; the yield of 1,5-hexanediamine was 87%, the yield of 2-methylpiperidine was 8%.
- a vertical tube reactor (diameter: 16 mm, filling height: 50 cm, oil-heated double jacket) was with 177 g (100 ml) of a basic cobalt full contact (CoO with 5% Mn2O3, 1.4% Na2O) in the form of 1 to 1, 5 mm split filled.
- the temperature was raised to 100 bar with simultaneous passage of 150 Nl / h of hydrogen gradually increased from 100 to 330 ° C within 23 h and then held at 330 ° C for 30 h.
- a tube reactor connected in front of the hydrogenation reactor (diameter: 16 mm, filling height: 50 cm, oil-heated double jacket), which was filled with 70.0 g (100 ml) of ⁇ -aluminum oxide in the form of 1.5 mm strands, was at a pressure of Pumped 250 bar and a temperature of 80 ° C per hour from bottom to top 20.5 g 5-oxo-hexanitrile (purity: 97.7%) and 100 g liquid ammonia. Then 100 Nl / h of hydrogen were fed in per hour and the discharge from the upstream imination reactor was passed through the hydrogenation reactor from bottom to top at a pressure of 250 bar and a temperature of 110 ° C. After depressurization to normal pressure, the ammonia was distilled off. According to gas chromatographic analysis of the hydrogenation output, the yield of 1,5-hexanediamine was 96%, 2-methylpiperidine was obtained in 2% yield.
- a vertical tube reactor (diameter: 16 mm, filling height: 50 cm, oil-heated double jacket) was with 176.7 g (100 ml) of a basic cobalt full contact (CoO with 5% Mn203, 1.4% Na2O) in the form of 1 to 1.5 mm split filled and reduced as in example 2.
- a basic cobalt full contact CoO with 5% Mn203, 1.4% Na2O
- a vertical tube reactor (diameter: 16 mm, filling height: 50 cm, oil-heated double jacket) was with 177 g (100 ml) of a basic cobalt full contact (CoO with 5% Mn2O3, 1.4% Na2O) in the form of 1 to 1, 5 mm split filled and reduced as in example 2.
- a basic cobalt full contact CoO with 5% Mn2O3, 1.4% Na2O
- a vertical tube reactor (diameter: 16 mm, filling height: 50 cm, oil-heated double jacket) was with 177 g (100 ml) of a basic cobalt full contact (CoO with 5% Mn2O3, 1.4% Na2O) in the form of 1 to 1, 5 mm split filled and reduced as in example 2.
- a basic cobalt full contact CoO with 5% Mn2O3, 1.4% Na2O
- a tube reactor connected in front of the hydrogenation reactor (diameter: 16 mm, filling height: 50 cm, oil-heated double jacket), which was filled with 63.5 g (100 ml) of titanium dioxide (anatase) in the form of 1.5 mm strands, was at a pressure of 250 bar and a temperature of 80 ° C per hour from bottom to top 10 g 4,4-dimethyl-5-oxo-hexanitrile (purity: 97.2%) and 195 g of liquid ammonia are pumped. Then 100 Nl / h of hydrogen were fed in per hour and the discharge from the upstream imination reactor was passed through the hydrogenation reactor from bottom to top at a pressure of 250 bar and a temperature of 110 ° C.
- a vertical tube reactor (diameter: 16 mm, filling height: 50 cm, oil-heated double jacket) was with 177 g (100 ml) of a basic cobalt full contact (CoO with 5% Mn2O3, 1.4% Na2O) in the form of 1 to 1, 5 mm split filled and reduced as in example 2.
- a basic cobalt full contact CoO with 5% Mn2O3, 1.4% Na2O
- a tube reactor connected in front of the hydrogenation reactor (diameter: 16 mm, filling height: 50 cm, oil-heated double jacket), which was filled with 63.5 g (100 ml) of titanium dioxide (anatase) in the form of 1.5 mm strands, was at a pressure of 250 bar and a temperature of 80 ° C per hour from bottom to top 10 g of 4-isopropyl-5-oxo-hexanitrile (purity: 95.7%) and 115 g of liquid ammonia. Then 100 Nl / h of hydrogen were fed in per hour and the discharge from the upstream imination reactor was passed through the hydrogenation reactor from bottom to top at a pressure of 250 bar and a temperature of 110 ° C.
Abstract
Description
Die vorliegende Erfindung betrifft ein neues Verfahren zur Herstellung von aliphatischen Pentan-1,5-diaminen aus gamma-Cyanoketonen sowie neue Pentan-1,5-diamine.The present invention relates to a new process for the preparation of aliphatic pentane-1,5-diamines from gamma-cyanoketones and new pentane-1,5-diamines.
Aus Chem. Ber. 3387 bis 3389 (1966) ist die Herstellung von 1,5-Diaminohexan aus 5-Oxocapronitril bekannt. Hiernach erhält man 1,5-Diaminohexan nur über die Zwischenstufe des Oxims, indem man zunächst 5-Oxocapronitril mit Hydroxylaminhydrochlorid in Gegenwart von wasserfreiem Natriumcarbonat zum 5-Oximinocapronitril umsetzt und dieses anschließend mit Lithiumaluminiumhydrid zum Diamin reduziert; die Gesamtausbeute beträgt 42 %. Direkte aminierende Hydrierung des 5-Oxo-capronitrils führt nach Angaben der Autoren zum Cyclisierungsprodukt, dem 2-Methylpiperidin.From Chem. Ber. 3387 to 3389 (1966) the production of 1,5-diaminohexane from 5-oxocapronitrile is known. Thereafter, 1,5-diaminohexane is obtained only via the intermediate stage of the oxime by first reacting 5-oxocapronitrile with hydroxylamine hydrochloride in the presence of anhydrous sodium carbonate to give 5-oximinocapronitrile and then reducing this to lithium diamine with lithium aluminum hydride; the overall yield is 42%. According to the authors, direct aminating hydrogenation of 5-oxo-capronitrile leads to the cyclization product, 2-methylpiperidine.
Die grundsätzliche Problematik der Cyclisierung zu Piperidinen bei der aminierenden Hydrierung von γ-Cyanoketonen ist in Houben-Weyl, Band 11/1, Seite 357 bis 359, beschrieben.The basic problem of cyclization to piperidines in the aminating hydrogenation of γ-cyanoketones is described in Houben-Weyl, Volume 11/1, pages 357 to 359.
Aus der EP-A-42 119 ist ein Verfahren zur Herstellung primärer Mono- und Diamine aus Oxoverbindungen, die gegebenenfalls auch weitere zur Reduktion befähigte Gruppen enthalten können, mit Ammoniak und Wasserstoff in Gegenwart bekannter Hydrierkatalysatoren beschrieben, bei dem man vor der Reaktion mit Ammoniak und Wasserstoff in Gegenwart von Hydrierkatalysatoren die Oxo-Verbindungen bei Temperaturen von 10 bis 200°C und Drücken von 1 bis 300 bar einer Vorreaktion mit Ammoniak in Gegenwart von anorganischen und organischen Ionenaustauschern in der Ammoniumform als Iminbildungskatalysatoren unterwirft. Die Anwendung des Verfahrens ist ausschließlich in den Beispielen für die aminierende Hydrierung von 3-Cyano-3,5,5-trimethyl-cyclohexanon (Isophoronnitril) und 2,2,6,6-Tetramethyl-4-piperidon (Triacetonamin) beschrieben. Bei der aminierenden Hydrierung von Isophoronnitril werden durch den Einsatz des organischen Ionenaustauschers Lewatit SPR 120 in der Iminierung geringfügige Ausbeuteverbesserungen gegenüber der nicht-katalysierten Fahrweise erzielt (vgl. Vergleichsbeispiel 3 in der EP-A-42 119: 90,3 % Ausbeute, mit Lewatit SPR 120: 93,9 bis 94,7 %).EP-A-42 119 describes a process for the preparation of primary mono- and diamines from oxo compounds, which may also contain other groups capable of reduction, with ammonia and hydrogen in the presence of known hydrogenation catalysts, in which prior to the reaction with ammonia and hydrogen in the presence of hydrogenation catalysts, the oxo compounds at temperatures from 10 to 200 ° C and pressures from 1 to 300 bar a prereaction with ammonia in the presence of inorganic and organic ion exchangers in the ammonium form as imine formation catalysts. The application of the process is described exclusively in the examples for the aminating hydrogenation of 3-cyano-3,5,5-trimethyl-cyclohexanone (isophoronenitrile) and 2,2,6,6-tetramethyl-4-piperidone (triacetonamine). In the aminating hydrogenation of isophoronenitrile, the use of the organic ion exchanger Lewatit SPR 120 in the imination results in slight improvements in yield compared to the non-catalyzed procedure (cf. Comparative Example 3 in the EP-A-42 119: 90.3% yield, with Lewatit SPR 120: 93.9 to 94.7%).
Es steht also bislang kein Verfahren zur Verfügung, nach dem offenkettige γ-Cyanoketone unter technisch praktikablen Bedingungen und mit wirtschaftlich befriedigenden Ausbeuten in die entsprechenden offenkettigen Pentan-1,5-diamine überführt werden können.So far, there is no process available according to which open-chain γ-cyanoketones can be converted into the corresponding open-chain pentane-1,5-diamines under technically practical conditions and with economically satisfactory yields.
Der vorliegenden Erfindung lag daher die Aufgabe zugrunde, ein Verfahren zur Herstellung von Pentan-1,5-diaminen zu finden, das den zuvor genannten Nachteilen abhilft, insbesondere aus γ-Cyanoketonen unter technisch praktikablen Bedingungen Pentan-1,5-diamine herzustellen, mit technisch befriedigende Ausbeuten bzw. Raum-Zeit- Ausbeuten und neue Pentan-1,5-diamine mit - im Vergleich zum bekannten 1,5-Hexandiamin - höherem Substitutionsgrad herzustellen.The present invention was therefore based on the object of finding a process for the preparation of pentane-1,5-diamines which alleviates the disadvantages mentioned above, in particular from producing γ-cyanoketones under technically practicable conditions, with technically satisfactory yields or space-time yields and new pentane-1,5-diamines with - compared to the known 1,5-hexanediamine - higher degree of substitution.
Demgemäß wurde ein neues und verbessertes Verfahren zur Herstellung von Pentan-1,5-diaminen der allgemeinen Formel I
in der
- R¹
- C₁- bis C₂₀-Alkyl, das gegebenenfalls durch ein bis vier heterocyclische Reste, C₂- bis C₈-Carbalkoxy, Carboxy, C₁- bis C₈-Alkylamino und/oder Hydroxy substiuiert ist, C₂- bis C₂₀-Alkenyl, C₃- bis C₂₀-Cycloalkyl, C₄- bis C₂₀-Cycloalkyl-alkyl, C₄- bis C₂₀-Alkyl-cycloalkyl, C₂- bis C₂₀-Alkoxyalkyl, C₂- bis C₈-Alkoxycarbonyl, C₁- bis C₂₀-Halogenalkyl, Aryl, C₇- bis C₂₀-Aralkyl, C₇- bis C₂₀-Alkylaryl und
- R², R³
- unabhängig voneinander Wasserstoff, C₁- bis C₂₀-Alkyl, das gegebenenfalls durch ein bis vier heterocyclische Reste, C₂- bis C₈-Carbalkoxy, Carboxy, C₁- bis C₈-Alkylamino und/oder Hydroxy substituiert ist, C₂- bis C₂₀-Alkenyl, C₃- bis C₂₀-Cycloalkyl, C₄- bis C₂₀-Cycloalkyl-alkyl, C₄- bis C₂₀-Alkyl-cycloalkyl, C₂- bis C₂₀-Alkoxyalkyl, C₂- bis C₈-Alkoxycarbonyl, C₁- bis C₂₀-Halogenalkyl, Aryl, C₇- bis C₂₀-Aralkyl, C₇- bis C₂₀-Alkylaryl bedeuten oder gemeinsam für eine gegebenfalls durch eine bis fünf C₁-bis C₄-Alkylgruppen substituierte C₄- bis C₇-Alkylenkette stehen,
in der die Substituenten R¹, R² und R³ die oben genannten Bedeutungen haben, welches dadurch gekennzeichnet ist, daß man in zwei räumlich voneinander getrennten Reaktionsräumen
- a) die Cyanoketone der Formel II in einem ersten Reaktionsraum mit überschüssigem Ammoniak an aciden Heterogenkatalysatoren bei Temperaturen von 20 bis 150°C und Drücken von 15 bis 500 bar umsetzt und
- b) die entstandenen Reaktionsprodukte in einem zweiten Reaktionsraum mit Wasserstoff in Gegenwart von überschüssigem Ammoniak an cobalt-, nickel-, ruthenium-, palladium- und/oder anderen edelmetallhaltigen Katalysatoren, gegebenenfalls mit basischen Komponenten oder auf basischen oder neutralen Trägern bei Temperaturen von 50 bis 180°C und Drücken von 30 bis 500 bar hydriert.
in der
- R¹'
- C₁- bis C₂₀-Alkyl, das gegebenenfalls durch ein bis vier heterocyclische Reste, C₂- bis C₈-Carbalkoxy, Carboxy, C₁- bis C₈-Alkylamino und/oder Hydroxy substiuiert ist, C₂- bis C₂₀-Alkenyl, C₂- bis C₂₀-Alkinyl, C₃- bis C₂₀-Cycloalkyl, C₄- bis C₂₀-Cycloalkyl-alkyl, C₄- bis C₂₀-Alkyl-cycloalkyl, C₂- bis C₂₀-Alkoxyalkyl, C₂- bis C₈-Alkoxycarbonyl, C₁- bis C₂₀-Halogenalkyl, Aryl, C₇- bis C₂₀-Aralkyl, C₇- bis C₂₀-Alkylaryl und
- R²', R³'
- unabhängig voneinander Wasserstoff, C₁- bis C₂₀-Alkyl, das gegebenenfalls durch ein bis vier heterocyclische Reste, C₂- bis C₈-Carbalkoxy, Carboxy, C₁- bis CAlkylamino und/oder Hydroxy substituiert ist, C₂- bis C₂₀-Alkenyl, C₂- bis C₂₀-Alkinyl, C₃- bis C₂₀-Cycloalkyl, C₄- bis C₂₀-Cycloalkyl-alkyl, C₄- bis C₂₀-Alkyl-cycloalkyl, C₂- bis C₂₀-Alkoxyalkyl, C₂- bis C₈-Alkoxycarbonyl, C₁- bis C₂₀-Halogenalkyl, Aryl, C₇- bis C₂₀-Aralkyl, C₇- bis C₂₀-Alkylaryl bedeuten oder gemeinsam für eine gegebenfalls durch eine bis fünf C₁- bis C₄-Alkylgruppen substituierte C₄- bis C₇-Alkylenkette stehen,
in the
- R¹
- C₁- to C₂₀-alkyl, which is optionally substituted by one to four heterocyclic radicals, C₂- to C₈-carbalkoxy, carboxy, C₁- to C₈-alkylamino and / or hydroxy, C₂- to C₂₀-alkenyl, C₃- to C₂₀- Cycloalkyl, C₄ to C₂₀ cycloalkyl alkyl, C₄ to C₂₀ alkyl cycloalkyl, C₂ to C₂₀ alkoxyalkyl, C₂ to C₈ alkoxycarbonyl, C₁ to C₂₀ haloalkyl, aryl, C₇ to C₂₀ aralkyl, C₇ to C₂₀ alkylaryl and
- R², R³
- independently of one another hydrogen, C₁- to C₂₀-alkyl, which is optionally substituted by one to four heterocyclic radicals, C₂- to C₈-carbalkoxy, carboxy, C₁- to C₈-alkylamino and / or hydroxy is, C₂- to C₂₀-alkenyl, C₃- to C₂₀-cycloalkyl, C₄- to C₂₀-cycloalkyl-alkyl, C₄- to C₂₀-alkyl-cycloalkyl, C₂- to C₂₀-alkoxyalkyl, C₂- to C₈-alkoxycarbonyl, C₁- to C₂₀-haloalkyl, aryl, C₇- to C₂₀-aralkyl, C₇- to C₂₀-alkylaryl or together represent a C₄ to C₇-alkylene chain optionally substituted by one to five C₁-C₄-alkyl groups,
in which the substituents R¹, R² and R³ have the meanings given above, which is characterized in that one in two spatially separate reaction spaces
- a) the cyanoketones of the formula II are reacted in a first reaction chamber with excess ammonia over acidic heterogeneous catalysts at temperatures from 20 to 150 ° C. and pressures from 15 to 500 bar and
- b) the reaction products formed in a second reaction space with hydrogen in the presence of excess ammonia over cobalt, nickel, ruthenium, palladium and / or other noble metal-containing catalysts, optionally with basic components or on basic or neutral supports at temperatures from 50 to 180 ° C and pressures from 30 to 500 bar hydrogenated.
in the
- R¹ '
- C₁- to C₂₀-alkyl, which is optionally substituted by one to four heterocyclic radicals, C₂- to C₈-carbalkoxy, carboxy, C₁- to C₈-alkylamino and / or hydroxy, C₂- to C₂₀-alkenyl, C₂- to C₂₀- Alkynyl, C₃- to C₂₀-cycloalkyl, C₄- to C₂₀-cycloalkyl-alkyl, C₄- to C₂₀-alkyl-cycloalkyl, C₂- to C₂₀-alkoxyalkyl, C₂- to C₈-alkoxycarbonyl, C₁- to C₂₀-haloalkyl, aryl, C₇ to C₂₀ aralkyl, C₇ to C₂₀ alkylaryl and
- R² ', R³'
- independently of one another hydrogen, C₁- to C₂₀-alkyl, which is optionally substituted by one to four heterocyclic radicals, C₂- to C₈-carbalkoxy, carboxy, C₁- to CAlkylamino and / or hydroxy, C₂- to C₂₀-alkenyl, C₂- bis C₂₀-alkynyl, C₃- to C₂₀-cycloalkyl, C₄- to C₂₀-cycloalkyl-alkyl, C₄- to C₂₀-alkyl-cycloalkyl, C₂- to C₂₀-alkoxyalkyl, C₂- to C₈-alkoxycarbonyl, C₁- to C₂₀-haloalkyl, Aryl, C₇- to C₂₀-aralkyl, C₇- to C₂₀-alkylaryl or together represent a C₄- to C₇-alkylene chain optionally substituted by one to five C₁- to C₄-alkyl groups,
Das erfindungsgemäße Verfahren läßt sich wie folgt in zwei räumlich voneinander getrennten Reaktionsräume durchführen:
- a) In einer ersten Verfahrensstufe setzt man die gamma-Cyanoketone mit überschüssigem Ammoniak um. Dabei hält man einen Druck von 15 bis 500 bar, vorzugsweise von 30 bis 350 bar und eine Temperatur von 20 bis 150°C, vorzugsweise von 30 bis 100°C ein. Die Kondensation wird in Gegenwart von aciden Heterogenkatalysatoren durchgeführt.
Als acide Heterogenkatalysatoren eignen sich Metallverbindungen mit Lewissäuren- oder Bröstedtsäure-Charakter wie z. B. Aluminiumoxid, Siliciumdioxid, Titandioxid, Zirkondioxid, ferner Phosphate, wie z. B. Aluminiumphosphate oder Silikate wie z. B. amorphe oder kristalline Alumosilikate. Bevorzugt verwendet man Aluminiumoxid, Titandioxid, Zirkondioxid und Siliciumdioxid, insbesondere Aluminiumoxid und Titandioxid. Die Acidität der Katalysatoren kann gegebenenfalls durch Dotierung mit Halogeniden erhöht werden. So finden z. B. auch halogendotierte Katalysatoren, wie Chlorid auf Aluminiumoxid oder Chlorid auf Titandioxid, Verwendung.
Bei der Umsetzung der γ-Cyanoketone an den aciden Heterogenkatalysatoren hält man eine Katalysatorbelastung von 0,01 bis 10, vorzugsweise 0,05 bis 7, besonders bevorzugt von 0,1 bis 5 kg Cyanoketon pro kg Katalysator und Stunde ein. Pro Mol Cyanoketon setzt man zweckmäßig, aber nicht zwingend 5 bis 500 Mol NH₃, bevorzugt 10 bis 400, besonders bevorzugt 20 bis 300 Mol ein. Die Umsetzung der gamma-Cyanoketone mit Ammoniak kann auch in der Anwesenheit von inerten Lösungsmitteln, wie Alkanolen oder Tetrahydrofuran erfolgen.
Die Umsetzung der γ-Cyanoketone läßt sich diskontinuierlich, bevorzugt kontinuierlich durchführen, z. B. in Druckbehältern oder Druckbehälterkaskaden. Nach einer besonders bevorzugten Ausführungsform werden die γ-Cyanoketone und NH₃ durch einen Rohrreaktor geleitet, in dem der Katalysator in Form eines festen Bettes angeordnet ist. - b) Das so erhaltene Produkt wird in einer zweiten Verfahrensstufe mit 3 bis 10 000 Moläquivalenten Wasserstoff, bevorzugt 4 bis 500, besonders bevorzugt 4.5 bis 200, gegebenenfalls nach Zufuhr von weiterem Ammoniak, einer katalytischen Hydrierung zugeführt.
Die Hydrierung wird vorzugsweise in flüssigem Ammoniak durchgeführt. Pro Mol in Stufe 1 eingesetztem gamma-Cyanoketon verwendet man 5 bis 500 Mol NH₃, bevorzugt 10 bis 400 Mol, besonders bevorzugt 20 bis 300 Mol. Der NH₃-Anteil kann gegebenenfalls durch Zufuhr von NH₃ auf den gewünschten Wert erhöht werden.
Man hydriert im allgemeinen bei einer Temperatur von 50 bis 180°C, bevorzugt von 60 bis 160°C, besonders bevorzugt von 70 bis 140°C und einem Druck von 30 bis 500 bar, bevorzugt von 50 bis 350 bar, besonders bevorzugt von 70 bis 300 bar.
Die Katalysatorbelastungen liegen zweckmäßig im Bereich von 0,01 bis 5 kg/(kg x h), bevorzugt bei 0,02 bis 2,5, besonders bevorzugt bei 0,05 bis 2 kg/(kg x h).
Bei der Hydrierung können prinzipiell alle gängigen Hydrierkatalysatoren eingesetzt werden, die Nickel, Cobalt, Eisen, Kupfer, Ruthenium, Palladium oder andere Edelmetalle der VIII. Nebengruppe des Periodensystems enthalten. Bevorzugt verwendet man Ruthenium-, Cobalt- oder Nickel-Katalysatoren. Besonders bevorzugt sind Ruthenium- und Cobalt-Katalysatoren. Die katalytisch aktiven Metalle können als Vollkontakte oder auf Trägern eingesetzt werden. Als solche Träger kommen z. B. Aluminiumoxid, Titandioxid, Zirkondioxid, Zinkoxid oder Magnesiumoxid/Aluminiumoxide in Frage, bevorzugt werden Hydrierkatalysatoren mit basischen Komponenten, wie Oxide und Hydroxide von Alkali- und Erdalkalimetallen. Besonders bevorzugt als basische Komponente sind Oxide bzw. Hydroxide der Alkalimetalle, wie z.B. die des Natriums. Die basische Komponente kann ggf. auch während des Hydrierprozesses zugeführt werden, z. B. als Lösung von Alkali- oder Erdalkalihydroxiden in Wasser.
Besonders bevorzugt verwendet man in der Hydrierung Cobalt, Nickel oder Ruthenium mit basischer Komponente.
Die Umsetzung führt man bevorzugt kontinuierlich, z. B. in druckfesten Rührbehältern oder in einer Rührbehälterkaskade durch.
In einer besonders bevorzugten Ausführungsform werden Rohrreaktoren eingesetzt, in denen das Hydriergut in Sumpf- oder Rieselfahrweise über ein fest angeordnetes Katalysatorbett geleitet wird.
- a) In a first process step, the gamma-cyanoketones are reacted with excess ammonia. A pressure of 15 to 500 bar, preferably of 30 to 350 bar and a temperature of 20 to 150 ° C., preferably is maintained from 30 to 100 ° C. The condensation is carried out in the presence of acidic heterogeneous catalysts.
Suitable acidic heterogeneous catalysts are metal compounds with Lewis acid or Bröstedtsäure character such. As aluminum oxide, silicon dioxide, titanium dioxide, zirconium dioxide, and also phosphates, such as. B. aluminum phosphates or silicates such. B. amorphous or crystalline aluminosilicates. Aluminum oxide, titanium dioxide, zirconium dioxide and silicon dioxide, in particular aluminum oxide and titanium dioxide, are preferably used. The acidity of the catalysts can optionally be increased by doping with halides. So find z. B. also halogen-doped catalysts, such as chloride on aluminum oxide or chloride on titanium dioxide, use.
When the γ-cyanoketones are reacted on the acidic heterogeneous catalysts, a catalyst load of 0.01 to 10, preferably 0.05 to 7, particularly preferably 0.1 to 5 kg of cyanoketone per kg of catalyst per hour is maintained. Per mole of cyanoketone is advantageously, but not necessarily, 5 to 500 moles of NH 3, preferably 10 to 400, particularly preferably 20 to 300 moles. The gamma cyanoketones can also be reacted with ammonia in the presence of inert solvents, such as alkanols or tetrahydrofuran.
The implementation of the γ-cyanoketones can be carried out batchwise, preferably continuously, for. B. in pressure vessels or pressure vessel cascades. According to a particularly preferred embodiment, the γ-cyanoketones and NH₃ are passed through a tubular reactor in which the catalyst is arranged in the form of a fixed bed. - b) The product obtained in this way is subjected to a catalytic hydrogenation in a second process stage with 3 to 10,000 molar equivalents of hydrogen, preferably 4 to 500, particularly preferably 4.5 to 200, if appropriate after the addition of further ammonia.
The hydrogenation is preferably carried out in liquid ammonia. 5 to 500 mol of NH₃, preferably 10 to 400 mol, particularly preferably 20 to 300 mol, are used per mol of gamma-cyanoketone used in stage 1. The NH₃ content can optionally be increased to the desired value by adding NH₃.
The hydrogenation is generally carried out at a temperature of 50 to 180 ° C., preferably 60 to 160 ° C., particularly preferably 70 to 140 ° C. and a pressure of 30 to 500 bar, preferably 50 to 350 bar, particularly preferably 70 up to 300 bar.
The catalyst loads are expediently in the range from 0.01 to 5 kg / (kg × h), preferably from 0.02 to 2.5, particularly preferably from 0.05 to 2 kg / (kg × h).
In principle, all common hydrogenation catalysts which contain nickel, cobalt, iron, copper, ruthenium, palladium or other noble metals of subgroup VIII of the periodic table can be used in the hydrogenation. Ruthenium, cobalt or nickel catalysts are preferably used. Ruthenium and cobalt catalysts are particularly preferred. The catalytically active metals can be used as full contacts or on supports. As such carriers come e.g. As aluminum oxide, titanium dioxide, zirconium dioxide, zinc oxide or magnesium oxide / aluminum oxides in question, hydrogenation catalysts with basic components such as oxides and hydroxides of alkali and alkaline earth metals are preferred. Oxides or hydroxides of alkali metals, such as, for example, sodium, are particularly preferred as the basic component. The basic component can optionally also be supplied during the hydrogenation process, e.g. B. as a solution of alkali or alkaline earth metal hydroxides in water.
Cobalt, nickel or ruthenium with a basic component are particularly preferably used in the hydrogenation.
The reaction is preferably carried out continuously, for. B. in pressure-resistant stirred tanks or in a stirred tank cascade.
In a particularly preferred embodiment, tubular reactors are used in which the hydrogenation product is passed over a fixed catalyst bed in a bottom or trickle mode.
Die Verfahrensstufen a und b können ebenfalls in einem Reaktor durchgeführt werden, in dem Iminierungskatalysatoren und Hydrierkatalysatoren in zwei getrennten Schichten angeordnet sind. In diesem Fall führt man die Iminierung zweckmäßigerweise in Gegenwart von Wasserstoff durch.Process steps a and b can also be carried out in a reactor in which imination catalysts and hydrogenation catalysts are arranged in two separate layers. In this case, the imination is advantageously carried out in the presence of hydrogen.
Nach der Hydrierung wird überschüssiges Ammoniak gegebenenfalls unter Druck abgetrennt. Die so erhaltenen Pentan-1,5-diamine lassen sich durch fraktionierende Destillation isolieren. Substituierte Piperidine entstehen nur in untergeordnetem Maße als Nebenprodukt.After the hydrogenation, excess ammonia is separated off, if appropriate under pressure. The pentane-1,5-diamines thus obtained can be isolated by fractional distillation. Substituted piperidines only arise to a minor extent as a by-product.
Die Ausgangsstoffe für das Verfahren, die γ-Cyanoketone, sind z.B. aus Ketonen und Acrylnitril zugänglich.The starting materials for the process, the γ-cyanoketones, are e.g. accessible from ketones and acrylonitrile.
Das erfindungsgemäße Verfahren ermäglicht hiermit die Umwandlung der γ-Cyanoketone in hohen Ausbeuten und Raum-Zeit-Ausbeuten zu den Pentan-1,5-diaminen.The process according to the invention thus enables the conversion of the γ-cyanoketones in high yields and space-time yields to the pentane-1,5-diamines.
Die Substituenten R¹, R² und R³ in den Verbindungen I und II haben folgende Bedeutungen:
- R¹, R², R³
-
- unverzweigtes oder verzweigtes C₁- bis C₂₀-Alkyl, bevorzugt C₁- bis C₈-Alkyl wie Methyl, Ethyl, n-Propyl, iso-Propyl, n-Butyl, iso-Butyl, sec.-Butyl, tert.-Butyl, n-Pentyl, iso-Pentyl, sec.-Pentyl, neo-Pentyl, 1,2-Dimethylpropyl, n-Hexyl, iso-Hexyl, sec.-Hexyl, n-Heptyl, iso-Heptyl, n-Octyl und iso-Octyl, besonders bevorzugt C₁- bis C₄-Alkyl wie Methyl, Ethyl, n-Propyl, iso-Propyl, n-Butyl, iso-Butyl, sec.-Butyl und tert.-Butyl,
- unverzweigtes oder verzweigtes C₁- bis C₂₀-Alkyl, das durch ein bis vier, bevorzugt ein bis drei, besonders ein oder zwei heterocyclische Reste, wie Pyridyl, und/oder C₂- bis C₈-Carbalkoxi, Carboxi, C₁- bis C₈-Alkylamino und/oder Hydroxy substituiert ist, bevorzugt Heteroaryl, besonders bevorzugt Pyridyl,
- C₂- bis C₂₀-Alkenyl, bevorzugt C₂- bis C₈-Alkenyl, besonders bevorzugt C₂- bis C₄-Alkenyl wie Vinyl, 1-Propenyl, 2-Propenyl, 1-Methylethenyl, 1-Butenyl, 2-Butenyl, 3-Butenyl, 1-Methyl-1-propenyl, 2-Methyl-1-propenyl, 1-Methyl-2-propenyl und 2-Methyl-2-propenyl;
- C₃- bis C₂₀-Cycloalkyl, bevorzugt C₃- bis C₈-Cycloalkyl wie Cyclopropyl, Cyclobutyl, Cyclopentyl, Cyclohexyl, Cycloheptyl und Cyclooctyl, besonders bevorzugt Cyclopropyl, Cyclopentyl, Cyclohexyl und Cyclooctyl,
- C₄- bis C₂₀-Cycloalkyl-alkyl, bevorzugt C₄- bis C₁₂-Cycloalkyl-alkyl, besonders bevorzugt C₄- bis C₈-Cyclo-alkyl-alkyl wie Cyclopentylmethyl und Cyclohexylmethyl;
- C₄- bis C₂₀-Alkyl-cycloalkyl, bevorzugt C₄- bis C₁₂-Alkyl-cycloalkyl, besonders bevorzugt C₄- bis C₈-Alkyl-Cycloalkyl wie Methyl-cyclopentyl und Methylcyclohexyl;
- C₁- bis C₂₀-Alkoxyalkyl, bevorzugt C₁- bis C₈-Alkoxyalkyl, besonders bevorzugt C₁- bis C₅-Alkoxyalkyl wie Methoxymethyl, Ethoxymethyl, n-Propoxymethyl, iso-Propoxy-methyl, n-Butoxymethyl, iso-Butoxymethyl, sec.-Butoxymethyl, tert.-Butoxymethyl und 1-Methoxy-ethyl,
- C₁- bis C₂₀-Halogenalkyl, bevorzugt C₁- bis C₈-Halogenalkyl, besonders bevorzugt C₁- bis C₄-Fluor- und/oder Chloralkyl wie Fluormethyl, Difluormethyl, Trifluormethyl, Chlormethyl, Dichlormethyl und Trichlormethyl,
- Aryl wie Phenyl, 1-Naphthyl, 2-Naphthyl, 1-Anthryl, 2-Anthryl und 9-Anthryl, bevorzugt Phenyl, 1-Naphthyl und 2-Naphthyl, besonders bevorzugt Phenyl,
- C₇- bis C₂₀-Aralkyl, bevorzugt C₇- bis C₁₂-Phenylalkyl wie Benzyl, 1-Phenethyl, 2-Phenethyl, 1-Phenyl-propyl, 2-Phenyl-propyl, 3-Phenyl-propyl, 1-Phenyl-butyl, 2-Phenyl-butyl, 3-Phenyl-butyl und 4-Phenyl-butyl, besonders bevorzugt Benzyl, 1-Phenethyl und 2-Phenethyl,
- C₇- bis C₂₀-Alkylaryl, bevorzugt C₇- bis C₁₂-Alkylphenyl wie 2-Methylphenyl, 3-Methylphenyl, 4-Methylphenyl, 2,4-Dimethyl-phenyl, 2,5-Dimethylphenyl, 2,6-Dimethylphenyl, 3,4-Dimethyl-phenyl, 3,5-Dimethylphenyl, 2,3,4-Trimethylphenyl, 2,3,5-Tri-methylphenyl, 2,3,6-Trimethylphenyl, 2,4,6-Trimethylphenyl, 2-Ethylphenyl, 3-Ethylphenyl, 4-Ethylphenyl, 2-n-Propylphenyl, 3-n-Propylphenyl und 4-n-Propylphenyl,
- C₂- bis C₈-Alkoxycarbonyl, bevorzugt C₁- bis C₄-Alkoxycarbonyl, besonders bevorzugt Methoxy und Ethoxycarbonyl.
- R² und R³
- zusätzlich unabhängig voneinander
- Wasserstoff
- gemeinsam für eine gegebenenfalls durch bis zu fünf C₁- bis C₄-Alkylgruppen substituierte cyclische oder acyclische C₁- bis C₇-Alkylenkette, wie z.B. =CH₂, =CH-CH₃, =C(CH₃)₂, -CH₂-CH₂-CH₂-, -(CH₂)₄-, -(CH₂)₅-, -(CH₂)₆-.
- R¹, R², R³
-
- unbranched or branched C₁ to C₂₀ alkyl, preferably C₁ to C₈ alkyl such as methyl, ethyl, n-propyl, isopropyl, n-butyl, isobutyl, sec-butyl, tert-butyl, n- Pentyl, iso-pentyl, sec.-pentyl, neo-pentyl, 1,2-dimethylpropyl, n-hexyl, iso-hexyl, sec.-hexyl, n-heptyl, iso-heptyl, n-octyl and iso-octyl, particularly preferred C₁ to C wie alkyl such as methyl, ethyl, n-propyl, iso-propyl, n-butyl, iso-butyl, sec-butyl and tert-butyl,
- unbranched or branched C₁- to C₂₀-alkyl by one to four, preferably one to three, especially one or two heterocyclic radicals, such as pyridyl, and / or C₂- to C₈-carbalkoxi, carboxi, C₁- to C₈-alkylamino and / or hydroxy is substituted, preferably heteroaryl, particularly preferably pyridyl,
- C₂ to C₂₀ alkenyl, preferably C₂ to C₈ alkenyl, particularly preferably C₂ to C₄ alkenyl such as vinyl, 1-propenyl, 2-propenyl, 1-methylethenyl, 1-butenyl, 2-butenyl, 3-butenyl, 1-methyl-1-propenyl, 2-methyl-1-propenyl, 1-methyl-2-propenyl and 2-methyl-2-propenyl;
- C₃- to C₂₀-cycloalkyl, preferably C₃- to C₈-cycloalkyl such as cyclopropyl, cyclobutyl, cyclopentyl, cyclohexyl, cycloheptyl and cyclooctyl, particularly preferably cyclopropyl, cyclopentyl, cyclohexyl and cyclooctyl,
- C₄- to C₂₀-cycloalkyl-alkyl, preferably C₄- to C₁₂-cycloalkyl-alkyl, particularly preferably C₄- to C₈-cycloalkyl-alkyl such as cyclopentylmethyl and cyclohexylmethyl;
- C₄ to C₂₀ alkyl cycloalkyl, preferably C₄ to C₁₂ alkyl cycloalkyl, particularly preferably C₄ to C₈ alkyl cycloalkyl such as methylcyclopentyl and methylcyclohexyl;
- C₁- to C₂₀-alkoxyalkyl, preferably C₁- to C₈-alkoxyalkyl, particularly preferably C₁- to C₅-alkoxyalkyl such as methoxymethyl, ethoxymethyl, n-propoxymethyl, iso-propoxy-methyl, n-butoxymethyl, iso-butoxymethyl, sec.-butoxymethyl , tert-butoxymethyl and 1-methoxy-ethyl,
- C₁ to C₂₀ haloalkyl, preferably C₁ to C₈ haloalkyl, particularly preferably C₁ to C₄ fluoro and / or chloroalkyl such as fluoromethyl, difluoromethyl, trifluoromethyl, chloromethyl, dichloromethyl and trichloromethyl,
- Aryl such as phenyl, 1-naphthyl, 2-naphthyl, 1-anthryl, 2-anthryl and 9-anthryl, preferably phenyl, 1-naphthyl and 2-naphthyl, particularly preferably phenyl,
- C₇ to C₂₀ aralkyl, preferably C₇ to C₁₂ phenylalkyl such as benzyl, 1-phenethyl, 2-phenethyl, 1-phenyl-propyl, 2-phenyl-propyl, 3-phenyl-propyl, 1-phenyl-butyl, 2-phenyl-butyl, 3-phenyl-butyl and 4-phenyl-butyl, particularly preferably benzyl, 1-phenethyl and 2-phenethyl,
- C₇ to C₂₀ alkylaryl, preferably C₇ to C₁₂ alkylphenyl such as 2-methylphenyl, 3-methylphenyl, 4-methylphenyl, 2,4-dimethylphenyl, 2,5-dimethylphenyl, 2,6-dimethylphenyl, 3,4 -Dimethylphenyl, 3,5-dimethylphenyl, 2,3,4-trimethylphenyl, 2,3,5-tri-methylphenyl, 2,3,6-trimethylphenyl, 2,4,6-trimethylphenyl, 2-ethylphenyl, 3 Ethylphenyl, 4-ethylphenyl, 2-n-propylphenyl, 3-n-propylphenyl and 4-n-propylphenyl,
- C₂- to C₈-alkoxycarbonyl, preferably C₁- to C₄-alkoxycarbonyl, particularly preferably methoxy and ethoxycarbonyl.
- R² and R³
- additionally independently of each other
- hydrogen
- together for a cyclic or acyclic C₁ to C₇ alkylene chain optionally substituted by up to five C₁ to C₄ alkyl groups, such as = CH₂, = CH-CH₃, = C (CH₃) ₂, -CH₂-CH₂-CH₂-, - (CH₂) ₄-, - (CH₂) ₅-, - (CH₂) ₆-.
Die Substituenten R¹' bis R³' in den Verbindungen I' haben die gleiche Bedeutung wie die Substituenten R¹ bis R³ in den Verbindungen I, mit der Maßgabe, daß R¹' nicht für Methyl steht, wenn R²' und R³' für Wasserstoff ist.The substituents R¹ 'to R³' in the compounds I 'have the same meaning as the substituents R¹ to R³ in the compounds I, with the proviso that R¹' is not methyl when R² 'and R³' is hydrogen.
Bevorzugte γ-Cyanoketone der allgemeinen Formel II sind z.B.:
5-Oxohexannitril (aus Aceton), 4-Methyl-5-oxo-hexannitril (aus Methylethylketon), 4-Methyl-5-oxo-heptannitril (aus Diethylketon), 4-Ethyl-5-oxo-hexannitril (aus Methylpropylketon), 4,4-Dimethyl-5-oxo-hexannitril (aus Methylisopropylketon), 4,4-Dimethyl-5-oxo-heptannitril (aus Ethylisopropylketon), 4,4,5-Trimethyl-5-oxo-heptannitril (aus Diisopropylketon), 4-Isoproypl-5-oxo-hexannitril (aus Methylisobutylketon), 4-Isopropenyl-5-oxo-hexannitril, 4-Isopropyliden-5-oxo-hexannitril (aus Methylisobutenylketon), 6,6-Dimethyl-5-oxo-heptannitril (aus Pinakolon), 4-Decyl-5-oxohexannitril (aus Methylundecylketon), 4-(3-Methyl-butyl)-5-oxo-hexannitril (aus 6-Methyl-2-heptanon), 4-iso-Butyl-5-oxo-hexannitril (aus 5-Methyl-2-hexanon), 4-Butyl-5-oxo-hexannitril (aus 2-Heptanon), 4-(2-Methyl-butyl)-5-oxo-hexannitril (aus 5-Methyl-2-heptanon), 5-Phenyl-5-oxo-pentannitril (aus Acetophenon), 4-Benzyl-5-oxo- hexannitril (aus 4-Phenyl-2-butanon), 4,6-Diphenyl-5-oxo-hexannitril (aus Dibenzylketon), 1-Acetyl-1-cyanethyl-cyclohexan (aus Cyclohexylmethylketon), 1-Acetyl-1-cyanethyl-cyclopropan (aus Cyclopropylmethylketon), 4,4-Dimethoxy-5-oxo-hexannitril (aus Methylglyoxaldimethylacetal), 4-Methoxy-5-oxo-hexannitril (aus Methoxyaceton), 5-Pyridyl-5-oxo-pentannitril (aus Acetylpyridin), 5-Methoxycarbonyl-5-oxo-pentannitril (aus Brenztraubensäuremethylester), 4-Methoxycarbonyl-5-oxo-hexannitril (aus Acetessigester).Preferred γ-cyanoketones of the general formula II are, for example:
5-oxohexanenitrile (from acetone), 4-methyl-5-oxo-hexanenitrile (from methyl ethyl ketone), 4-methyl-5-oxo-heptanenitrile (from diethyl ketone), 4-ethyl-5-oxo-hexanenitrile (from methyl propyl ketone), 4,4-dimethyl-5-oxo-hexanenitrile (from methyl isopropyl ketone), 4,4-dimethyl-5-oxo-heptanenitrile (from ethyl isopropyl ketone), 4,4,5-trimethyl-5-oxo-heptanenitrile (from diisopropyl ketone), 4-isoproypl-5-oxo-hexanenitrile (from methyl isobutyl ketone), 4-isopropenyl-5-oxo-hexanenitrile, 4-isopropylidene-5-oxo-hexanenitrile (from methyl isobutenyl ketone), 6,6-dimethyl-5-oxo-heptanenitrile (from pinacolone), 4-decyl-5-oxohexanenitrile (from methylundecyl ketone), 4- (3-methylbutyl) -5-oxo-hexanenitrile (from 6-methyl-2 -heptanone), 4-iso-butyl-5-oxo-hexanenitrile (from 5-methyl-2-hexanone), 4-butyl-5-oxo-hexanenitrile (from 2-heptanone), 4- (2-methyl-butyl ) -5-oxo-hexanenitrile (from 5-methyl-2-heptanone), 5-phenyl-5-oxo-pentanenitrile (from acetophenone), 4-benzyl-5-oxo-hexanenitrile (from 4-phenyl-2-butanone ), 4,6-Diphenyl-5-oxo-hexanenitrile (from dibenzyl ketone), 1-acetyl-1-cyanoethyl-cyclohexane (from cyclohexyl methyl ketone), 1-acetyl-1-cyanoethyl cyclopropane (from cyclopropyl methyl ketone), 4,4- Dimethoxy-5-oxo-hexanenitrile (from methylglyoxaldimethyl acetal), 4-methoxy-5-oxo-hexanenitrile (from methoxyacetone), 5-pyridyl-5-oxo-pentanenitrile (from acetylpyridine), 5-methoxycarbonyl-5-oxo-pentanenitrile ( from methyl pyruvate), 4-methoxycarbonyl-5-oxo-hexanenitrile (from acetoacetic ester).
Bevorzugte Pentan-1,5-diamine der Formeln I und I' sind: Hexan-1,5-diamin, 4-Methyl-hexan-1,5-diamin, 4-Methyl-heptan-1,5-diamin, 4-Ethyl-hexan-1,5-diamin, 4,4-Dimethyl-hexan-1,5-diamin, 4,4-Dimethyl-heptan-1,5-diamin, 4,4,6,Trimethyl-heptan-1,5-diamin, 4-Isopropyl-hexan-1,5-diamin, 6,6-Dimethyl-heptan-1,5-diamin, 4-Decyl-hexan-1,5-diamin, 4-(3-Methyl-butyl)-hexan-1,5-diamin, 4-iso-Butyl-hexan-1,5-diamin, 4-Butyl-hexan-1,5-diamin, 4-(2-Methyl-butyl)-hexan-1,5-diamin, 1-Phenyl-pentan-1,5-diamin, 4-Benzyl-hexan-1,5-diamin, 4,6-Diphenyl-hexan-1,5-diamin, 1-(1-Aminoethyl)-1-(3-aminopropyl)-cyclohexan, 1-(1-Aminoethyl)-1-(3-aminopropyl)-cyclopropan, 4,4-Dimethoxy-hexan-1, 5-diamin, 4-Methoxy-hexan-1, 5-diamin, 5-Pyridyl-pentan-1,5-diamin, 5-Methoxycarbonyl-pentan-1,5-diamin, 4-Methoxycarbonyl-hexan- 1,5-diamin.Preferred pentane-1,5-diamines of the formulas I and I 'are: hexane-1,5-diamine, 4-methyl-hexane-1,5-diamine, 4-methyl-heptane-1,5-diamine, 4- Ethyl-hexane-1,5-diamine, 4,4-dimethyl-hexane-1,5-diamine, 4,4-dimethyl-heptane-1,5-diamine, 4,4,6, trimethyl-heptane-1, 5-diamine, 4-isopropyl-hexane-1,5-diamine, 6,6-dimethyl-heptane-1,5-diamine, 4-decyl-hexane-1,5-diamine, 4- (3-methyl-butyl ) -hexane-1,5-diamine, 4-iso-butyl-hexane-1,5-diamine, 4-butyl-hexane-1,5-diamine, 4- (2-methyl-butyl) -hexane-1, 5-diamine, 1-phenylpentane-1,5-diamine, 4-benzyl-hexane-1,5-diamine, 4,6-diphenyl-hexane-1,5-diamine, 1- (1-aminoethyl) - 1- (3-aminopropyl) -cyclohexane, 1- (1-aminoethyl) -1- (3-aminopropyl) -cyclopropane, 4,4-dimethoxy-hexane-1,5-diamine, 4-methoxy-hexane-1, 5-diamine, 5-pyridyl-pentane-1,5-diamine, 5-methoxycarbonyl-pentane-1,5-diamine, 4-methoxycarbonyl-hexane-1,5-diamine.
Die beanspruchten Diamine zeichnen sich gegenüber dem bekannten 1,5-Hexandiamin auf Grund des höheren Substitutionsgrades durch geringere Flüchtigkeit und stärkere Asymmetrie (unterschiedliche Reaktivität der Aminfunktionen) aus. Daraus resultieren u.a. leichte Verarbeitbarkeit der Diamine, beispielsweise als Komponenten (Härter) für Epoxide und Komponenten für Polyamide und geringere Geruchsbelästigungen durch unumgesetzte Diamine sowie der daraus herstellbaren Diisocyanate.The claimed diamines are distinguished from the known 1,5-hexanediamine by virtue of the higher degree of substitution by lower volatility and greater asymmetry (different reactivity of the amine functions). This results in easy processing of the diamines, for example as components (hardeners) for epoxies and components for polyamides and less odor nuisance due to unreacted diamines and the diisocyanates that can be produced from them.
Ein vertikaler Rohrreaktor (Durchmesser: 16 mm, Füllhöhe: 50 cm, ölbeheizter Doppelmantel) wurde mit 90,1 g (87 ml) eines Katalysators mit 3 % Ruthenium auf β-Aluminiumoxid in Form von 1,2 mm-Strängen gefüllt (Katalysatorherstellung durch Porentränkung von β-Aluminiumoxid mit wäßriger Rutheniumnitrat-Lösung und Trocknen bei 120°C). Der Katalysator wurde zur Reduktion bei 100 bar unter gleichzeitigem Durchleiten von 150 Nl/h Wasserstoff nach schrittweiser Erhöhung der Temperatur von 100 auf 220°C innerhalb von 7 h 9 h bei 220°C gehalten.A vertical tubular reactor (diameter: 16 mm, filling height: 50 cm, oil-heated double jacket) was filled with 90.1 g (87 ml) of a catalyst with 3% ruthenium on β-aluminum oxide in the form of 1.2 mm strands (catalyst preparation by Pore impregnation of β-aluminum oxide with aqueous ruthenium nitrate solution and drying at 120 ° C). The catalyst was kept at 100 bar for reduction with simultaneous passage of 150 Nl / h of hydrogen after gradually increasing the temperature from 100 to 220 ° C. within 7 h 9 h at 220 ° C.
Durch einen vor den Hydrierreaktor geschalteten Rohrreaktor (Durchmesser: 16 mm, Füllhöhe: 50 cm, ölbeheizter Doppelmantel), der mit 65.3 g (100 ml) Titandioxid (Anatas) in Form von 1.5 mm-Strängen gefüllt war, wurden bei einem Druck von 250 bar und einer Temperatur von 80°C stündlich 20.5 g 5-Oxo-hexannitril (Reinheit 97.7 %) und 240 g flüssiger Ammoniak gepumpt. Der Austrag wurde anschlieáend bei einem Druck von 250 bar und einer Temperatur von 110°C unter gleichzeitigem Durchleiten von 100 Nl/h Wasserstoff von unten nach oben durch den Hydrierreaktor geleitet. Nach Entspannen auf Normaldruck wurde NH₃ abdestilliert und der Hydrieraustrag mit quantitativer Gaschromatographie analysiert; es ergab sich eine Ausbeute an 1,5-Hexandiamin von 87 %, die Ausbeute an 2-Methylpiperidin betrug 8 %.A tube reactor (diameter: 16 mm, filling height: 50 cm, oil-heated double jacket), which was filled with 65.3 g (100 ml) of titanium dioxide (anatase) in the form of 1.5 mm strands, was passed through a tube reactor upstream of the hydrogenation reactor at a pressure of 250 bar and a temperature of 80 ° C, 20.5 g of 5-oxo-hexanenitrile (purity 97.7%) and 240 g of liquid ammonia are pumped every hour. The discharge was then passed through the hydrogenation reactor from bottom to top at a pressure of 250 bar and a temperature of 110 ° C. while simultaneously passing 100 Nl / h of hydrogen through it. After relaxing to normal pressure, NH₃ was distilled off and the hydrogenation output was analyzed with quantitative gas chromatography; the yield of 1,5-hexanediamine was 87%, the yield of 2-methylpiperidine was 8%.
Ein vertikaler Rohrreaktor (Durchmesser: 16 mm, Füllhöhe: 50 cm, ölbeheizter Doppelmantel) wurde mit 177 g (100 ml) eines basischen Cobalt-Vollkontaktes (CoO mit 5 % Mn₂O₃, 1,4 % Na₂O) in Form von 1 bis 1,5 mm Split gefüllt. Zur Reduktion des Katalysators wurde bei 100 bar unter gleichzeitigem Durchleiten von 150 Nl/h Wasserstoff die Temperatur innerhalb von 23 h schrittweise von 100 auf 330°C erhöht und dann 30 h bei 330°C gehalten.A vertical tube reactor (diameter: 16 mm, filling height: 50 cm, oil-heated double jacket) was with 177 g (100 ml) of a basic cobalt full contact (CoO with 5% Mn₂O₃, 1.4% Na₂O) in the form of 1 to 1, 5 mm split filled. To reduce the catalyst, the temperature was raised to 100 bar with simultaneous passage of 150 Nl / h of hydrogen gradually increased from 100 to 330 ° C within 23 h and then held at 330 ° C for 30 h.
Durch einen vor den Hydrierreaktor geschalteten Rohrreaktor (Durchmesser:. 16 mm, Füllhöhe: 50 cm, ölbeheizter Doppelmantel), der mit 70.0 g (100 ml) γ-Aluminiumoxid in Form von 1.5-mm-Strängen gefüllt war, wurden bei einem Druck von 250 bar und einer Temperatur von 80°C stündlich von unten nach oben 20,5 g 5-Oxo-hexannitril (Reinheit: 97,7 %) und 100 g flüssiger Ammoniak gepumpt. Anschließend wurden stündlich 100 Nl/h Wasserstoff zugefahren und der Austrag aus dem vorgeschalteten Iminierungsreaktor bei einem Druck von 250 bar und einer Temperatur von 110°C von unten nach oben durch den Hydrierreaktor gefahren. Nach Entspannen auf Normaldruck wurde der Ammoniak abdestilliert. Laut gaschromatographischer Analyse des Hydrieraustrages betrug die Ausbeute an 1,5-Hexandiamin 96 %, 2-Methylpiperidin entstand mit 2 % Ausbeute.A tube reactor connected in front of the hydrogenation reactor (diameter: 16 mm, filling height: 50 cm, oil-heated double jacket), which was filled with 70.0 g (100 ml) of γ-aluminum oxide in the form of 1.5 mm strands, was at a pressure of Pumped 250 bar and a temperature of 80 ° C per hour from bottom to top 20.5 g 5-oxo-hexanitrile (purity: 97.7%) and 100 g liquid ammonia. Then 100 Nl / h of hydrogen were fed in per hour and the discharge from the upstream imination reactor was passed through the hydrogenation reactor from bottom to top at a pressure of 250 bar and a temperature of 110 ° C. After depressurization to normal pressure, the ammonia was distilled off. According to gas chromatographic analysis of the hydrogenation output, the yield of 1,5-hexanediamine was 96%, 2-methylpiperidine was obtained in 2% yield.
Ein vertikaler Rohrreaktor (Durchmesser: 16 mm, Füllhöhe: 50 cm, ölbeheizter Doppelmantel) wurde mit 176,7 g (100 ml) eines basischen Cobalt-Vollkontaktes (CoO mit 5 % Mn₂0₃, 1,4 % Na₂O) in Form von 1 bis 1,5 mm Split gefüllt und wie in Beispiel 2 reduziert.A vertical tube reactor (diameter: 16 mm, filling height: 50 cm, oil-heated double jacket) was with 176.7 g (100 ml) of a basic cobalt full contact (CoO with 5% Mn₂0₃, 1.4% Na₂O) in the form of 1 to 1.5 mm split filled and reduced as in example 2.
Durch einen vor den Hydrierreaktor geschalteten Rohrreaktor (Durchmesser: 16 mm, Füllhöhe: 20 cm, ölbeheizter Doppelmantel), der mit 25.4 g (40 ml) Titandioxid (Anatas) in Form von 1,5-mm-Strängen gefüllt war, wurden bei einem Druck von 250 bar und einer Temperatur von 80°C stündlich von unten nach oben 20,5 g 5-Oxo-hexannitril (Reinheit: 97,7 %) und 340 g flüssiger Ammoniak gepumpt. Anschließend wurden stündlich 100 Nl/h Wasserstoff zugefahren und der Austrag aus dem vorgeschalteten Iminierungsreaktor bei einem Druck von 250 bar und einer Temperatur von 110°C von unten nach oben durch den Hydrierreaktor gefahren. Nach Entspannen auf Normaldruck wurde der Ammoniak abdestilliert und der Hydrieraustrag aus 75 Stunden durch fraktionierende Destillation über eine 30 cm Füllkörperkolonne (3 mm Glasringe) aufgetrennt. Mann erhält 1400 g 1,5-Hexandiamin, entsprechend einer Ausbeute von 89 %.Through a tubular reactor connected in front of the hydrogenation reactor (diameter: 16 mm, filling height: 20 cm, oil-heated double jacket), which was filled with 25.4 g (40 ml) titanium dioxide (anatase) in the form of 1.5 mm strands, Pressure of 250 bar and a temperature of 80 ° C per hour from bottom to top 20.5 g of 5-oxo-hexanitrile (purity: 97.7%) and 340 g of liquid ammonia pumped. Then 100 Nl / h of hydrogen were fed in per hour and the discharge from the upstream imination reactor was passed through the hydrogenation reactor from bottom to top at a pressure of 250 bar and a temperature of 110 ° C. After releasing the pressure to atmospheric pressure, the ammonia was distilled off and the hydrogenation was carried out for 75 hours by fractional distillation over a 30 cm packed column (3 mm glass rings) separated. 1400 g of 1,5-hexanediamine are obtained, corresponding to a yield of 89%.
Ein vertikaler Rohrreaktor (Durchmesser: 16 mm, Füllhöhe: 50 cm, ölbeheizter Doppelmantel) wurde mit 177 g (100 ml) eines basischen Cobalt-Vollkontaktes (CoO mit 5 % Mn₂O₃, 1,4 % Na₂O) in Form von 1 bis 1,5 mm Split gefüllt und wie in Beispiel 2 reduziert.A vertical tube reactor (diameter: 16 mm, filling height: 50 cm, oil-heated double jacket) was with 177 g (100 ml) of a basic cobalt full contact (CoO with 5% Mn₂O₃, 1.4% Na₂O) in the form of 1 to 1, 5 mm split filled and reduced as in example 2.
Durch einen vor den Hydrierreaktor geschalteten Rohrreaktor (Durchmesser: 0. 16 mm, Füllhöhe: 50 cm, ölbeheizter Doppelmantel), der mit 63.5 g (100 ml) Titandioxid (Anatas) in Form von 1.5-mm-Strängen gefüllt war, wurden bei einem Druck von 250 bar und einer Temperatur von 80°C stündlich von unten nach oben 21 g 4,4-Dimethyl-5-oxo-hexannitril (Reinheit: 97,2 %) und 180 g flüssiger Ammoniak gepumpt. Anschließend wurden stündlich 100 Nl/h Wasserstoff zugefahren und der Austrag aus dem vorgeschalteten Iminierungsreaktor bei einem Druck von 250 bar und einer Temperatur von 110°C von unten nach oben durch den Hydrierreaktor gefahren. Nach Entspannen auf Normaldruck wurde der Ammoniak abdestilliert. Der Austrag aus 24 Stunden wurde durch fraktionierende Destillation über eine 30 cm Füllkörperkolonne (3 mm Glasringe) aufgetrennt. Man erhält 445 g 4,4-Dimethyl-1,5-hexandiamin als farblose Flüssigkeit (Sdp. 90°C/3 mbar), entsprechend einer Ausbeute von 88 %.Through a tube reactor connected in front of the hydrogenation reactor (diameter: 0.16 mm, filling height: 50 cm, oil-heated double jacket), which was filled with 63.5 g (100 ml) of titanium dioxide (anatase) in the form of 1.5 mm strands, Pressure of 250 bar and a temperature of 80 ° C per hour from bottom to top 21 g of 4,4-dimethyl-5-oxo-hexanitrile (purity: 97.2%) and 180 g of liquid ammonia pumped. Then 100 Nl / h of hydrogen were fed in per hour and the discharge from the upstream imination reactor was passed through the hydrogenation reactor from bottom to top at a pressure of 250 bar and a temperature of 110 ° C. After depressurization to normal pressure, the ammonia was distilled off. The discharge from 24 hours was separated by fractional distillation over a 30 cm packed column (3 mm glass rings). 445 g of 4,4-dimethyl-1,5-hexanediamine are obtained as a colorless liquid (bp. 90 ° C./3 mbar), corresponding to a yield of 88%.
Ein vertikaler Rohrreaktor (Durchmesser: 16 mm, Füllhöhe: 50 cm, ölbeheizter Doppelmantel) wurde mit 177 g (100 ml) eines basischen Cobalt-Vollkontaktes (CoO mit 5 % Mn₂O₃, 1,4 % Na₂O) in Form von 1 bis 1,5 mm Split gefüllt und wie in Beispiel 2 reduziert.A vertical tube reactor (diameter: 16 mm, filling height: 50 cm, oil-heated double jacket) was with 177 g (100 ml) of a basic cobalt full contact (CoO with 5% Mn₂O₃, 1.4% Na₂O) in the form of 1 to 1, 5 mm split filled and reduced as in example 2.
Durch einen vor den Hydrierreaktor geschalteten Rohrreaktor (Durchmesser: 16 mm, Füllhöhe: 50 cm, ölbeheizter Doppelmantel), der mit 63.5 g (100 ml) Titandioxid (Anatas) in Form von 1.5-mm-Strängen gefüllt war, wurden bei einem Druck von 250 bar und einer Temperatur von 80°C stündlich von unten nach oben 10 g 4,4-Dimethyl-5-oxo-hexannitril (Reinheit: 97,2 %) und 195 g flüssiger Ammoniak gepumpt. Anschließend wurden stündlich 100 Nl/h Wasserstoff zugefahren und der Austrag aus dem vorgeschalteten Iminierungsreaktor bei einem Druck von 250 bar und einer Temperatur von 110°C von unten nach oben durch den Hydrierreaktor gefahren. Nach Entspannen auf Normaldruck wurde der Ammoniak abdestilliert und der Hydrieraustrag mittels gaschromatographie quantitativ analysiert; es ergab sich eine Ausbeute von 93.0 % an 4,4-Dimethyl-1,5-hexandiamin und 4.5 % an 2,3,3-Trimethylpiperidin.A tube reactor connected in front of the hydrogenation reactor (diameter: 16 mm, filling height: 50 cm, oil-heated double jacket), which was filled with 63.5 g (100 ml) of titanium dioxide (anatase) in the form of 1.5 mm strands, was at a pressure of 250 bar and a temperature of 80 ° C per hour from bottom to top 10 g 4,4-dimethyl-5-oxo-hexanitrile (purity: 97.2%) and 195 g of liquid ammonia are pumped. Then 100 Nl / h of hydrogen were fed in per hour and the discharge from the upstream imination reactor was passed through the hydrogenation reactor from bottom to top at a pressure of 250 bar and a temperature of 110 ° C. After depressurization to normal pressure, the ammonia was distilled off and the hydrogenation output was analyzed quantitatively by means of gas chromatography; there was a yield of 93.0% of 4,4-dimethyl-1,5-hexanediamine and 4.5% of 2,3,3-trimethylpiperidine.
Ein vertikaler Rohrreaktor (Durchmesser: 16 mm, Füllhöhe: 50 cm, ölbeheizter Doppelmantel) wurde mit 177 g (100 ml) eines basischen Cobalt-Vollkontaktes (CoO mit 5 % Mn₂O₃, 1,4 % Na₂O) in Form von 1 bis 1,5 mm Split gefüllt und wie in Beispiel 2 reduziert. Durch einen vor den Hydrierreaktor geschalteten Rohrreaktor (Durchmesser: 16 mm, Füllhöhe: 50 cm, ölbeheizter Doppelmantel), der mit 63.5 g (100 ml) Titandioxid (Anatas) in Form von 1.5-mm-Strängen gefüllt war, wurden bei einem Druck von 250 bar und einer Temperatur von 80°C stündlich von unten nach oben 10 g 4-Isopropyl-5-oxo-hexannitril (Reinheit: 95,7 %) und 115 g flüssiger Ammoniak gepumpt. Anschließend wurden stündlich 100 Nl/h Wasserstoff zugefahren und der Austrag aus dem vorgeschalteten Iminierungsreaktor bei einem Druck von 250 bar und einer Temperatur von 110°C von unten nach oben durch den Hydrierreaktor gefahren. Nach Entspannen auf Normaldruck wurde der Ammoniak abdestilliert und der Austrag aus 72 Stunden durch fraktionierende Destillation über eine 30 cm Füllkörperkolonne (3 mm Glasringe) aufgetrennt. Man erhält 640 g 4-Isopropyl-1,5-hexandiamin als farblose Flüssigkeit (Sdp. 80°C/ 1 mbar), entsprechend einer Ausbeute von 90 %.A vertical tube reactor (diameter: 16 mm, filling height: 50 cm, oil-heated double jacket) was with 177 g (100 ml) of a basic cobalt full contact (CoO with 5% Mn₂O₃, 1.4% Na₂O) in the form of 1 to 1, 5 mm split filled and reduced as in example 2. A tube reactor connected in front of the hydrogenation reactor (diameter: 16 mm, filling height: 50 cm, oil-heated double jacket), which was filled with 63.5 g (100 ml) of titanium dioxide (anatase) in the form of 1.5 mm strands, was at a pressure of 250 bar and a temperature of 80 ° C per hour from bottom to top 10 g of 4-isopropyl-5-oxo-hexanitrile (purity: 95.7%) and 115 g of liquid ammonia. Then 100 Nl / h of hydrogen were fed in per hour and the discharge from the upstream imination reactor was passed through the hydrogenation reactor from bottom to top at a pressure of 250 bar and a temperature of 110 ° C. After releasing the pressure to atmospheric pressure, the ammonia was distilled off and the discharge from 72 hours by fractional distillation through a 30 cm packed column (3 mm glass rings). 640 g of 4-isopropyl-1,5-hexanediamine are obtained as a colorless liquid (b.p. 80 ° C./1 mbar), corresponding to a yield of 90%.
Claims (9)
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE4129350A DE4129350A1 (en) | 1991-09-04 | 1991-09-04 | METHOD FOR PRODUCING PENTANE-1,5-DIAMINES |
| DE4129350 | 1991-09-04 |
Publications (3)
| Publication Number | Publication Date |
|---|---|
| EP0530696A2 true EP0530696A2 (en) | 1993-03-10 |
| EP0530696A3 EP0530696A3 (en) | 1993-05-19 |
| EP0530696B1 EP0530696B1 (en) | 1995-08-09 |
Family
ID=6439808
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| EP92114711A Expired - Lifetime EP0530696B1 (en) | 1991-09-04 | 1992-08-28 | Process for the preparation of pentane 1,5-diamines |
Country Status (6)
| Country | Link |
|---|---|
| US (1) | US5344983A (en) |
| EP (1) | EP0530696B1 (en) |
| JP (1) | JPH05238991A (en) |
| CA (1) | CA2076917A1 (en) |
| DE (2) | DE4129350A1 (en) |
| ES (1) | ES2075550T3 (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5395972A (en) * | 1993-02-08 | 1995-03-07 | Sumitomo Chemical Company, Limited | Process for producing amines |
| US5589596A (en) * | 1993-04-27 | 1996-12-31 | Sumitomo Chemical Company, Limited | Process for producing amines |
| US10214615B2 (en) | 2012-08-24 | 2019-02-26 | Croda International Plc | Polyimide composition |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR2292698A1 (en) * | 1974-11-07 | 1976-06-25 | Ciba Geigy Ag | CURING MIXTURES BASED ON POLYEPOXIDES CONTAINING CERTAIN DIAMINO-DECANES |
| EP0010179A1 (en) * | 1978-09-25 | 1980-04-30 | Ruhrchemie Aktiengesellschaft | Process for the preparation of 2.2-dialkylpentane-1.5-diamines, and the compounds N-(4-cyano-2.2-diethylbutyl)-4-cyano-2.2-dimethyl butylidene imine and N-(4-cyano-2-n-butyl-2-ethylbutyl)-4-cyano-2-n-butyl-2-ethyl-butylidene imine |
| EP0042119A2 (en) * | 1980-06-12 | 1981-12-23 | Hüls Aktiengesellschaft | Process for the preparation of primary mono- and diamines from oxo-compounds |
| EP0077105A1 (en) * | 1981-10-10 | 1983-04-20 | Stamicarbon B.V. | Diisocyanate |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| NL6910764A (en) * | 1969-07-11 | 1971-01-13 | ||
| US4054553A (en) * | 1975-06-02 | 1977-10-18 | General Electric Company | Polyphenylene oxide process |
| DE3028384A1 (en) * | 1980-07-26 | 1982-02-25 | Basf Ag, 6700 Ludwigshafen | METHOD FOR PRODUCING N-ALKYLPIPERIDINES AND N-ALKYLPYRROLIDINES |
-
1991
- 1991-09-04 DE DE4129350A patent/DE4129350A1/en not_active Withdrawn
-
1992
- 1992-08-26 CA CA002076917A patent/CA2076917A1/en not_active Abandoned
- 1992-08-26 US US07/936,084 patent/US5344983A/en not_active Expired - Lifetime
- 1992-08-28 ES ES92114711T patent/ES2075550T3/en not_active Expired - Lifetime
- 1992-08-28 EP EP92114711A patent/EP0530696B1/en not_active Expired - Lifetime
- 1992-08-28 DE DE59203203T patent/DE59203203D1/en not_active Expired - Lifetime
- 1992-09-01 JP JP4233593A patent/JPH05238991A/en not_active Withdrawn
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR2292698A1 (en) * | 1974-11-07 | 1976-06-25 | Ciba Geigy Ag | CURING MIXTURES BASED ON POLYEPOXIDES CONTAINING CERTAIN DIAMINO-DECANES |
| EP0010179A1 (en) * | 1978-09-25 | 1980-04-30 | Ruhrchemie Aktiengesellschaft | Process for the preparation of 2.2-dialkylpentane-1.5-diamines, and the compounds N-(4-cyano-2.2-diethylbutyl)-4-cyano-2.2-dimethyl butylidene imine and N-(4-cyano-2-n-butyl-2-ethylbutyl)-4-cyano-2-n-butyl-2-ethyl-butylidene imine |
| EP0042119A2 (en) * | 1980-06-12 | 1981-12-23 | Hüls Aktiengesellschaft | Process for the preparation of primary mono- and diamines from oxo-compounds |
| EP0077105A1 (en) * | 1981-10-10 | 1983-04-20 | Stamicarbon B.V. | Diisocyanate |
Non-Patent Citations (1)
| Title |
|---|
| CHEMISCHE BERICHTE Bd. 99, 1966, WEINHEIM DE Seiten 3387 - 3389 G. VITA, G. BUCHER 'Notiz zur Darstellung aliphatischer Diamine' * |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5395972A (en) * | 1993-02-08 | 1995-03-07 | Sumitomo Chemical Company, Limited | Process for producing amines |
| US5589596A (en) * | 1993-04-27 | 1996-12-31 | Sumitomo Chemical Company, Limited | Process for producing amines |
| US10214615B2 (en) | 2012-08-24 | 2019-02-26 | Croda International Plc | Polyimide composition |
Also Published As
| Publication number | Publication date |
|---|---|
| EP0530696B1 (en) | 1995-08-09 |
| JPH05238991A (en) | 1993-09-17 |
| US5344983A (en) | 1994-09-06 |
| EP0530696A3 (en) | 1993-05-19 |
| CA2076917A1 (en) | 1993-03-05 |
| DE59203203D1 (en) | 1995-09-14 |
| ES2075550T3 (en) | 1995-10-01 |
| DE4129350A1 (en) | 1993-03-11 |
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